CN1250677C - Waste plastic oiling device for continuous industrial production at large scale - Google Patents
Waste plastic oiling device for continuous industrial production at large scale Download PDFInfo
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- CN1250677C CN1250677C CNB2004100580183A CN200410058018A CN1250677C CN 1250677 C CN1250677 C CN 1250677C CN B2004100580183 A CNB2004100580183 A CN B2004100580183A CN 200410058018 A CN200410058018 A CN 200410058018A CN 1250677 C CN1250677 C CN 1250677C
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- Prior art keywords
- coke discharging
- oil
- gas
- coke
- jar
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/005—Coking (in order to produce liquid products mainly)
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
Abstract
The present invention relates to a device for changing waste plastic into oil in continuous industrialization production. The present invention comprises a reaction kettle, a feeding device, a heating device, a coke discharging device, a fractionating-steam stripping-condensing and cooling device, a gas-oil separation-gas absorber, a petroleum product extracting refining device and a liquid gas recovery device, wherein the feeding device is connected with the reaction kettle; the heating device supplies the reaction for the reaction kettle; the coke discharging device is arranged at the bottom of the reaction kettle; the fractionating-steam stripping-condensing and cooling device, the gas-oil separation-gas absorber, the petroleum product extracting refining device and the liquid gas recovery device are orderly connected behind the reaction kettle; the liquid gas recovery device is led out by the gas-oil separation-gas absorber. The present invention is characterized in that the present invention also comprises three waste processing devices, wherein the three waste processing devices has the functions of fume deinking dust removal and waste oil and waste water treatment recovery; the fume deinking dust removing device is connected with a smoke channel outlet of the heating device; the waste oil and waste water treatment recovery device is connected with the petroleum product extracting refining device; the feeding device comprises a hot pressing thickening roll device and a high temperature seal feeding device; the heating device is a non open flame panel heating device; the coke discharging device comprises at least three interlocking coke discharging sliding valves. The present invention can be used for cracking and changing the waste plastic into the oil, can be suitable for producing high quality fuel oil or the fractions of gasoline and diesel oil by cracking and lighting waste lubricating oil and heavy oil, and can be suitable for recovering liquid gas, etc.
Description
Technical field
But the present invention relates to a kind of plastic waste oilization device that utilizes plastic waste or waste lubricating oil or heavy wet goods to produce the continuous industry production of gasoline fraction, diesel oil distillate or high-quality fuel oil and civil liquefied gas by catalysis or on-catalytic cracking.
Background technology
Relevant both at home and abroad plastic waste oiling Study on Technology with develop the history that had for two more than ten years, it is divided into catalysis and on-catalytic cracking two big classes.But when forming large-scale continuous industrial production, all run into the Processes and apparatus problem of same difficulty.Up at present, the large-scale commercial production device of still rarer serialization both at home and abroad, long-term operation is gone into operation.The main technique plant issue that runs into has six kinds: the first high temperature feeding equipment: how designing the complete feeding equipment of a cover can be under cracking high temperature, in the inflammable and explosive atmosphere, the plastic waste of carrying certain proportion silt dust and moisture content secretly is added in the reactor, is the primary plant issue that serialization production runs into.The second high temperature residue extraction mechanism: residue extraction mechanism how to design a cover safety can be in the scission reaction process, and the cinder that the sediment contamination of the suspension that produces during with fusing and reaction produce is in time discharged reactor, also is to form the prerequisite that serialization is produced.The 3rd reaction heat supply problem, how to design the reaction heating furnace of the non-naked light heating of a cover, it can satisfy the requirement that improves flame temperature and yield of radiation, and enough reaction heat is provided, and must obey the design specifications requirement of inflammable and explosive pressurized vessel no open flames heating again.The 4th designs the refinement treatment equipment of the effective cracked oil of a cover, to product decolour, deodorizing, stable, make it the all-mass index and reach the GB requirement.Can produce waste gas, waste water, waste residue inevitably in the 5th technological process, how design the effective secondary pollution treatment facility of a cover, they be handled eliminate in device inside, also be important process and the plant issue that can device survive.The equipment of the guaranteed safety production measures of the 6th design; this mainly is meant in inflammable and explosive high-temperature reaction process; how to guarantee that being perfectly safe of high temperature continuous charging and deslagging is reliable; return catch fire prevention and put out, the container overpressure protection, stop tempering etc., hardware device and measure of gas shiled, deslagging as reinforced.
At present, Japanese fuji reclaims company and POKODA group company energy goods and materials reproducing unit etc. and is is researching and developing plastic waste oiling technology, and its characteristics one are that plastic waste will pass through careful sorting, washing oven dry, extrusion molding shaping etc., and treatment process is very complicated huge; Another characteristics are that fusing is carried out respectively with cracking, but problems such as molten plastic solidifying when carrying in the pump housing and in the pipeline are not resolved.Also have the exploitation that also conducting a research energetically of some companies, but all fail to form plant-scale production equipment.
Once there was the research and development group headed by the Midi Ta Gexiai of University of Kentucky (Mehdi Taghiei) professor in the U.S., was engaged in many researchs, had obtained experimental research achievements, had affirmed that plastic waste can make the theory and the experiment feasibility of high-quality fuel oil through cracking.But they are the methods with hydrogenation catalyst, and technology is very complicated.
Britain BP company and the European Community 5 tame oil companies, once pounced on blue strange this refinery of lance to have built a cover processing power be the small test device of 100kg/h in 1993 in Scotland, this is the pyrolysis device of a cover fluidized-bed sand stove.It is to be ejected in 400～900 ℃ of pyritous sand fluidized-bed reaction stills cleaning the plastic waste fine debris of pulverizing, and is cracked into the hydrocarbon mixture based on ethene, propylene.Ethene, propylene will can be used as polyethylene, polypropylene monomer through precision fractional distillation and after handling.But even to this day, there is no the large-scale industry device goes into operation.
Domestic situation, indigenous oil refining still formula cracking little Reaktionsofen is a lot, and majority can't be realized continuous operation, can not realize the high temperature continuous charging, more can't the high temperature deslagging, but a still one still ground carries out; Its oil production color depth, stink is big, character is unstable, and quality does not reach national standard; Secondary pollution is comparatively serious, and waste water and dregs waste gas discharges everywhere; Production safety, personnel safety lack capable measure, do not ensure.
Summary of the invention
At above-mentioned variety of issue, but the purpose of this invention is to provide a kind of plastic waste oilization device of continuous industry production.
For achieving the above object, the present invention takes following technical scheme: but a kind of plastic waste oilization device of continuous industry production, it comprises: reactor, the feeding unit that connects described reactor, heating unit for described reactor reaction, be arranged on the coke discharging device of described reactor bottom, be connected to described reactor fractionation-stripping-condensation refrigerating unit afterwards in turn, gas-oil separation-gas absorbing device, oil product extracting and refining device, and the liquefied gas retrieving arrangement of drawing by gas-oil separation-gas absorbing device; It is characterized in that: it also comprises by having flue gas takes off the three wastes processing unit of black dedusting and waste oil waste water treatment and reclamation function, described flue gas takes off the flue outlet that black cleaning apparatus connects described heating unit, the waste oil waste water treatment and reclamation device of described " three wastes " treatment unit connects described oil product extracting and refining device, described waste oil waste water treatment and reclamation device comprises oil trap and water-and-oil separator, the water side of described oil trap connects described water-and-oil separator by lift pump, the water side of described water-and-oil separator connects described recirculation water shower nozzle by the outer water circulating pump of described gas wash tower, the oil outlet end of described oil trap and water-and-oil separator is connected back described reactor, continues cracking; The flue gas of described " three wastes " treatment unit takes off black gas wash tower and is divided into two sections, epimere is spray quinoline gas wash tower, hypomere is the water seal dedusting absorption tower, described gas wash tower is outside equipped with water circulating pump, be provided with the recirculation water shower nozzle in the described gas wash tower, described gas wash tower stage casing is provided with dividing plate, and described dividing plate lower-most point is provided with fluid flow tube; Described feeding unit comprises hot pressing density roll device and elevated-temperature seal feeding device two portions, described hot pressing density roll device comprises chapelet, the flue gas chuck stove that is connected with chapelet, be arranged on track type chain making machine and hot pressing density roll stacks in the described chuck stove, be arranged on the conveying belt below the described hot pressing density roll stacks, be arranged on the water-cooling-sprayer of described conveying belt top and gantry chopper that described conveying belt exports is set, be arranged on the cooling basin of described chopper below and the scraper-type chain making machine that sets within it to described elevated-temperature seal feeding device convey materials.Described heating unit is non-naked light radiation formula heating unit, and described coke discharging device is made up of the coke discharging guiding valve of 2～3 coke discharging jars and 3 interlockings.
The present invention comprises that also one is arranged on the plastic breaker between described hot pressing density roll device and the elevated-temperature seal feeding device, and one is arranged on before the described reactor and carries the tubular oven of hot waste oil and mink cell focus to described reactor.
Described elevated-temperature seal feeding device comprises by frequency control motor drive lift, be connected described lift and the band stirrer loading hopper between the blanking inclined tube, the reinforced forcing machine of molten formula is moulded in the sealing that connects described loading hopper, described forcing machine comprises the pushing screw rod that is driven by frequency control motor and is looped around described pushing screw rod barrel on every side, be provided with heating flue gas chuck in the exit of described forcing machine, vertical connection one casing drum in the exit of described forcing machine, the top of described casing drum is provided with one and discloses the material mechanical manipulator, and the bottom of described casing drum is connected described reactor by the thermal expansion joint with the valve that feeds in raw material.
Described non-naked light radiation formula heating unit comprises the roasting kiln that is arranged on the marmon clamp blind roaster around the described reactor and is arranged on described reactor bottom, one annular is led flame cover or six and is led flame tube and be communicated with described marmon clamp blind roaster and roasting kiln, on described roasting kiln, be provided with one deck resistance flame plate, and described resistance flame plate is provided with the resistance flame aperture that is evenly distributed, both sides at described roasting kiln are provided with a burner respectively, the crater of described burner tilts along the furnace wall direction, the flame of ejection is formed in burner hearth revolve flame.
Described high temperature interlocking coke discharging device comprises one-level coke discharging jar and the secondary coke discharging jar that the first coke discharging guiding valve on the coke discharging tube is connected bottom described reactor, be connected second guiding valve between the described I and II coke discharging jar and be connected the 3rd guiding valve below the secondary coke discharging jar, described three guiding valve interlocking coke dischargings, described one-level coke discharging jar are provided with two coke discharging mechanical manipulators and and visit burnt mechanical manipulator.
Described high temperature interlocking coke discharging device comprises the coke discharging jar of the conversion operation of three parallel connections, wherein a positive coke discharging jar be arranged on the same axis of the coke discharging tube of described reactor on, in addition the central axis of two described coke discharging jars and described positive coke discharging jar is an angle and is arranged on and arranged on left and right sides, and the downward-sloping first-class burnt gradient of two coke discharging jars difference about described, described three coke discharging jars connect the coke discharging tube of described reactor respectively by a coke discharging guiding valve, and described three guiding valve interlocking coke dischargings, described each coke discharging jar is provided with a coke discharging mechanical manipulator.
The present invention is owing to take above technical scheme, it has the following advantages: 1, the present invention is owing to be provided with hot pressing density roll device in feeding device, and in hot pressing density roll device, be provided with flue gas chuck stove, chain making machine, roll stacks, conveying belt, gantry chopper, cooling basin and the chain making machine in the pond, therefore can transmit in the process of plastic waste its heating at chain making machine, and rolling through hot pressing density roll stacks, form one by pressure rolling plastic tape closely, plastic tape can be lowered the temperature by water-cooling-sprayer in the conveying belt outlet again simultaneously, and be cut into plastics fritter than specification by gantry chopper, deliver to next procedure by the chain making machine in the cooling basin then, particularly be provided with crusher and plastics can also be cut into more tiny particle, solved the problem of the processing in early stage of the plastic waste that has certain proportion silt dust effectively.2, the present invention is provided with the flue gas chuck at the outlet of extruder end of elevated-temperature seal feeding device, plastic waste is plastified or melt by flue gas heating to enter reactor, reduces the obstruction that lumpy material forms; The material mechanical manipulator is disclosed in setting on casing drum top, the artificial or reinforced obstruction of processing or not smooth automatically by mechanical manipulator; In the blanking inclined tube, electronic monitor system is set, cooperates with the setter of lift to monitor and regulate the blanking flow state; Be provided with in extruding machine barrel and return gas temperature-sensitive alarm element, sender is closed reinforced guiding valve at any time, prevents to return gas and takes place; The thermal expansion joint is set in the casing drum bottom,, alleviates influence, but above measures makes the reinforced safer more reliable more serialization ground operation of elevated-temperature seal the reactor thermal load with the stress that absorption is expanded with heat and contract with cold and produced.3, the present invention is owing to be provided with the tubular oven of preheating waste oil and mink cell focus before reactor, therefore, the present invention not only can be used for the plastic waste oiling, but also can be used for the lightweight oiling of waste lubricating oil or mink cell focus, produce high-quality fuel oil or gasoline, diesel cut, and both can be used for catalytic pyrolysis process, can be used for the on-catalytic cracking process again.4, the present invention owing to adopted is provided with around the marmon clamp blind roaster of reactor and is arranged on the roasting kiln of reactor bottom, and big by flow section, resistance is little, the annular that can guarantee combustion chamber draft is led the flame cover or six lead flame tube connected ring clevis blind roaster and roasting kiln, simultaneously by resistance flame plate is set in roasting kiln, on resistance flame plate, equally distributed resistance flame aperture is set, therefore realized reactor is carried out the radioactive even heating mode of non-naked light, not only improve heating efficiency, and reduced the coking of reactor bottom.5, the present invention is owing to be provided with the interlocking coke discharging device at least three reference mark, therefore, can guarantee the flowable state operation of reactor, in the operational process of reactor, unlatching by each guiding valve, close, realize the interlocking coke discharging, particularly on each coke discharging jar, be provided with the burnt mechanical manipulator of strand, can in time discharge various stopping states, guarantee carrying out smoothly of coke discharging.6, the present invention comprises that flue gas takes off black gas wash tower, oil trap and efficient water-and-oil separator owing to be provided with one, therefore the useless flue gas that roasting kiln produces can be sprayed and the water seal dedusting, after enter in the environment again, reduce environmental pollution, simultaneously can be with the waste oil water sepn, water purification back is continued to use for gas wash tower, oil is returned reactor continue cracking, thereby solved " the three wastes " the handling problem that this liquefying apparatus faces effectively.Particularly working as increase of the present invention and be provided with waste gas cinder boiler, can also be fuel with the cinder and the unnecessary gas of apparatus of the present invention output, produces steam etc.
Description of drawings
Fig. 1 is a system and device synoptic diagram of the present invention
Fig. 2 is a plastic waste hot pressing density roll device structural representation of the present invention
Fig. 3 is an elevated-temperature seal feeding device structural representation of the present invention
Fig. 4 is flowable state reactor of the present invention and non-naked light radiation furnace structural representation
Fig. 5 is the another kind of structural representation of flowable state reactor of the present invention and non-naked light radiation furnace
Fig. 6 is a high temperature interlocking coke discharging apparatus structure synoptic diagram of the present invention
Fig. 7 is the another kind of structural representation of high temperature interlocking coke discharging device of the present invention
Fig. 8 is fractionation-stripping of the present invention-condensation refrigerating unit structural representation
Fig. 9 is gas-oil separation of the present invention-gas absorbing device structural representation
Figure 10 is a liquefied gas retrieving arrangement structural representation of the present invention
Figure 11 is an oil product extracting and refining apparatus structure synoptic diagram of the present invention
Figure 12 is the present invention's " three wastes " treatment unit structural representation
Embodiment
As shown in Figure 1, but the cracking waste plastics device of the present invention's serialization large-scale commercial production comprises: hot pressing density roll device 1, elevated-temperature seal feeding device 2, flowable state reactor device 3, non-naked light radiation formula heating unit 4, high temperature interlocking coke discharging device 5, fractionation-stripping-condensation refrigerating unit 6, gas-oil separation-gas absorbing device 7, liquefied gas retrieving arrangement 8, oil product extracting and refining device 9 and " three wastes " treatment unit 10 etc.Described in detail respectively below.
As shown in Figure 1 and Figure 2, the newly-increased hot pressing density roll device 1 that is provided with of the present invention comprises and is arranged on top chapelet 101, what be connected with chapelet 101 is flue gas chuck stove 102, the interlayer baker that chuck stove 102 provides the inside and outside double-layer structure of heat to form by fume waste heat.Chuck stove 102 internal layers are provided with the track type chain making machine 103 of driven by motor, crawler belt on the chain making machine 103 will be sent into hot pressing density roll stacks 104 backward from the plastic waste that chapelet 101 is sent into, chuck stove 102 skins are provided with flue gas chuck burner hearth, utilize the hot flue gas of introducing from smoke inlet 105 to warm plastic waste on the chain making machine 103 to softening temperature.The control thermocouple 106 and the variable valve 107 on the smoke inlet 105 that are arranged on roll stacks 104 tops can be controlled plastics softening rolling temperature automatically.Being arranged on conveying belt 108 below the roll stacks 104 will be sent into gantry chopper 109 that is installed in its rear portion by roll stacks 104 rolling good softening plastic strips and be cut into small pieces, above conveying belt 108, be provided with a water-cooling-sprayer 110, make the softening plastic strip cooling hardening that shuts out by roll stacks 104, be convenient to cut hand hay cutter, prevent adhesion.Cut the cooling basin 111 that the plastics fritter that falls falls into chopper 109 bottoms from chopper 109, chopper 109 incision frequencies can be regulated according to desired stripping and slicing size, be arranged on the scraper-type chain making machine 112 in the pond 111, cooled plastics fritter can be delivered in the follow-up equipment on the bank of pond 111, the gap of the rotating speed of chain making machine 103 and roll stacks 104 all can be set to regulate may command.
As Fig. 1, shown in Figure 3, elevated-temperature seal feeding device 2 of the present invention comprises and is arranged on forward lift 201 that it is driven by frequency control motor 202, utilizes buncher 202 and setter 203, the size of may command feed amount.Blanking inclined tube 204 is connecting lift 201 and the loading hopper 205 of being with stirrer, electronic monitor system 206 is arranged on blanking inclined tube 204 stage casings, monitoring the smooth situation of blanking, and the information that is monitored sent constantly into setter 203, thereby regulate the pusher speed of lift 201 feed amounts and blanking inclined tube 204.Elevated-temperature seal is moulded the reinforced forcing machine 207 of molten formula and is arranged under the loading hopper 205, and forcing machine 207 comprises the pushing screw rod 209 that is driven by frequency control motor 208 and is looped around pushing screw rod 209 barrel 210 on every side.The use of frequency control motor 208 makes the easier control of pusher rotating speed, makes the ground operation of reinforced forcing machine 207 safety and reliability, for reinforced automatization provides assurance, and can prevent the generation of accident or the generation of termination accident in time.The characteristics of forcing machine 207 also are embodied in its exit and are provided with flue gas chuck 211, plastic waste are plastified or melt by flue gas heating to enter reactor 301.Casing drum 212 is vertically mounted on reactor 301 cover heads, connecting forcing machine 207 and reactor 301, the top of casing drum 212 is provided with one and discloses material mechanical manipulator 213, and mechanical manipulator 213 ends are provided with reamer 214, the usefulness of mediation processing when the generation casing drum bottom plastic of making provision against emergencies is jammed.Thermal expansion joint 218 is arranged on the bottom of casing drum 212, the stress that expands with heat and contract with cold and produced with absorption, this stress is because when operation, high temperature makes reactor 301 thermal expansions and up extends 10～30mm, and on the fixing steelframe at normal temperatures in forcing machine 207 bases, produce huge stress, have destructiveness, the setting of thermal expansion joint 218 has solved this problem well.Forcing machine 207 middle parts are provided with monitor alarm thermal sensing element 215, when just in case the cracking high-temperature oil gas take place return when scurrying back forcing machine to the middle part, warning thermal sensing element 215 will send signal immediately and give setter 216, setter 216 becomes the frequency transformer that send again sender to give the buncher 208 of reinforced forcing machine 207 through overregulating, automatically regulate the pusher rotating speed of variable-frequency motor 208, the acceleration pusher is blocked and is returned gas; If can't prevent, then will close charging valve 217 rapidly, send out signal simultaneously and stop forcing machine 207 and lift 201.Scurry elimination when oil gas returns, supervision thermal sensing element 215 will be sent out signal and give variable-frequency motor 208, start forcing machine 207 and lift 201, open charging valve 217 subsequently, recover normally operation.
As Fig. 1, shown in Figure 4, flowable state reactor device 3 of the present invention comprises flowable state reactor 301, be provided with upper and lower two-layer stirring rake 302,303 in the reactor 301, orthogonal stirring rake 302 and arcual stirring rake 303 are the cross grade separation (schematically the two being drawn in the plane among the figure) are set, the present invention puts unlike the prior art and is embodied in: all blade both sides of stirring rake 302,303 bands are provided with the edge of a knife, with cinder piece in the broken liquid or fritted unit of plastic.This has just solved in the past, and cinder piece and plastics clinker break paddle in the design, stop up coke discharging tube or make agitator motor moment excess load and trip, or cause problem such as reactor judder.Reactor 301 bottom sides are provided with the coke discharging tube 304 of band anti-coking chuck, and it can prevent that high-temperature flue gas from burning coke discharging tube, and heavy oil guarantees the coke discharging free pathway in the tube wall coking in avoiding managing.Oil-catalyst slurry feeding device 305 is arranged on reactor 301 tops, and it is made up of two sections sealing chamber and top feeding funnel three parts, and the hypomere sealing chamber is equipped with resistant to elevated temperatures sheet glass liquidometer, adds speed with the control catalyst oar.Reactor 301 tops are provided with a broken foam vaporization section 306, in the broken foam gasification section 306 grid support plate and Pall ring are housed.Vaporization section 306 tops are provided with the cooling water coil 307 of a generation internal reflux and the light oil return line 308 of external reflux are provided, and the casing drum 212 that reactor 301 tops are provided with is with 207 one-tenth 90 ° of vertical installations of charging forcing machine.
As Fig. 4, shown in Figure 5, non-naked light radiation formula heating unit 4 of the present invention is arranged on below the reactor 301, and is linked to be an integral body with reactor 301.It comprises a stove skirt 401, one annular is set around skirt 401 leads flame 402 (as shown in Figure 4) of cover or six and lead flame tube 403 (as shown in Figure 5), the marmon clamp blind roaster 404 that is provided with around the reactor 301 and the roasting kiln 405 of reactor 301 bottoms are led 402 or six in flame cover by annular and are led flame tube 403 and be connected.Heating unit of the present invention is embodied in various reacting furnace differences in the past: lead 402 or six flow sections of leading flame tube 403 of flame cover greater than more than 2 times of reactor 301 surrounded jacket stoves 404 cross sections.This has just reduced the resistance to flow that flue gas dwindles the cross section suddenly by the roomy flow volume of burner hearth, guarantees the vacuum tightness of burner hearth and good state of combustion, prevents that burner hearth from producing malleation, provides assurance for improving fire box temperature.This design has solved in the past that to lead the flame tube flow section in the design little, causes resistance big, and burner hearth vacuum tightness is low, even pressure combustion often takes place, and the flame fire door of emerging is dangerous, and has limited the raising of fire box temperature, makes problems such as reaction heat supply deficiency.Lead the upper and lower joints of flame tube 403 and be provided with waveform thermal expansion joint 406 (as Fig. 4, shown in Figure 5) leading 402 or six in flame cover,, guarantee that body of heater normally moves in order to absorb thermal expansion stress.Slack loop seriously leaked out during this structure had solved and designed in the past, and burner hearth vacuum tightness is reduced, and the bad problem of burning had both solved the absorption thermal expansion stress, had guaranteed the burner hearth sealing problem again.Be provided with the radiation resistance flame plate 407 that one deck is made by high temperature resistant (more than 1000 ℃) material of high radiance on the roasting kiln 405, and resistance flame plate 407 is provided with some resistance flame apertures that are evenly distributed, resistance flame plate 407 can prevent the direct contact reacts still 301 of flame, forms the radiation heating mode of non-naked light.This design of the present invention combines with the aforementioned big flame cross-sectional passage structure of leading, both can allow very high fire box temperature, guarantee that fully the reactor heat supply needs, can guarantee the safe operation of producing again, and fundamentally solve the problem of the Vessel Design code requirement that inflammable and explosive reactor can not the naked light heating.The burner 408 that roasting kiln 405 uses is the oil-gas mixed burning type; have functions such as automatic igniting, flame monitoring, blowout protection; it is arranged on the burner hearth hypomere and on grey thorax; two burners are separately positioned on the both sides of roasting kiln 405; and make into rim furnace wall direction; the flame of ejection is formed in burner hearth revolve flame, make being heated of resistance flame plate 407 more even.Top at reactor marmon clamp blind roaster 404 is provided with exhanst gas outlet 409, the flue gas of deriving to reduce phlegm and internal heat the chuck stove 102 of pressing density roll device 1 and the flue gas chuck 211 of elevated-temperature seal feeding device 2, and other needs the equipment of flue gas heating, flue gas finally is admitted to " three wastes " treatment unit 10 to carry out flue gas and takes off black the processing, and what discharge from chimney at last will be water vapor, nitrogen and carbonic acid gas.
As Fig. 1, shown in Figure 6, high temperature interlocking coke discharging device 5 of the present invention is arranged on a side of reactor 301, and it is made up of one-level coke discharging jar 501 and secondary coke discharging jar 502.Coke discharging tube 304 by the strap clamp cover between one-level coke discharging jar 501 and the reactor 301 is connected.Coke discharging tube 304 is provided with the first road coke discharging guiding valve 503.Be provided with the second road guiding valve 504 between the I and II coke discharging jar 501,502, be provided with the 3rd road guiding valve 505 below the secondary coke discharging jar 502.Three road valves 503,504,505 one-tenth interlocking state operations, promptly under the standard state, guiding valve 503 is for often leaving, and guiding valve 504 and 505 is a normally off.Interlocking coke discharging program is as follows: the first step is closed guiding valve 503 when having deposited a certain amount of burnt oar in the one-level coke discharging jar 501, cuts off and being connected of reactor 301, and guarantees deslagging safety, and three road guiding valves all are in closing condition at this moment; Second step, open guiding valve 504, make the cinder in 501 enter secondary coke discharging jar 502, the 3rd step, close guiding valve 504, open guiding valve 505, aperture is 10～30%, make its deslagging gradually, fall into wedged bottom coke discharging pond 506, and the cooled cinder piece of condensation in the water is reaped on the ground by chain scraper machine (not shown).So constantly repeat above-mentioned deslagging three steps, constantly discharge the cinder that generates in the reaction, assurance device moves continuously.Three mechanical manipulators 507,508,509 are separately positioned on the top and the side of one-level coke discharging jar 501, the top head of mechanical manipulator 507,509 is provided with a thin burnt drilling rod with centre-bit respectively, mechanical manipulator 509 is through to coke discharging tube 304 and reactor 301 bottoms, before the valve of mechanical manipulator 507 straight-through guiding valves 505.Mechanical manipulator 508 bottoms are garden dish, with the long-pending burnt situation in burnt jar 501 bottoms of monitoring one-level.Mechanical manipulator 507,508,509 can be controlled automatically, also can manually control.
As Fig. 1, shown in Figure 7, high temperature interlocking coke discharging device 5 of the present invention can also adopt the bull structure, and it is to be provided with three cover coke discharging jars 510,511,512 in parallel with above-mentioned single head interlocking coke discharging device difference, can conversion operation, flexible operating strengthens the coke discharging flow.Positive coke discharging jar 510 be arranged on reactor 301 same medullary rays on, link to each other with coke discharging tube 305 by coke discharging guiding valve 513, level is twisted burnt bar 514 and is arranged on coke discharging jar 510 and the coke discharging tube 305 same axis.Left and right sides coke discharging jar 511,512 is arranged on left and right about the 30 ° position of coke discharging jar 510 central axis horizontal sextant angles, its structure is identical with coke discharging jar 510, but left and right sides coke discharging jar 511,512 is designed to have the burnt gradient of a constant current, the central axis and the horizontal sextant angle that are the coke discharging tube 514,515 of coke discharging jar 511,512 are 5～15 ° of downward angle mounts, it is dirty to help burnt oar, prevents that coke is at coke discharging tube 514,515 pipe bottom sediments.
As Fig. 1, shown in Figure 8, fractionation-stripping of the present invention-condensation refrigerating unit 6 comprises that the bottom has the separation column 601 of flue gas chuck 602 as thermal source, and the bottom is provided with grid support plate 603 in the separation column 601, is supporting to fill the efficient Pall ring filler 604 in the tower.Be provided with heavy gas oil oil header 605 in the tower from bottom to top and extract line side line 606, solar oil oil header 607 and extraction line side line 608, kerosene oil header 609 and extraction side line 610 thereof out.Tower is outer to be provided with gasoline refluxing opening 611 from cat head, kerosene refluxing opening 612, solar oil refluxing opening 613, heavy gas oil refluxing opening 614 and heavy oil refluxing opening 615 at the bottom of tower.Kerosene stripping tower 616, solar oil stripping tower 617, heavy gas oil stripping tower 618 is overlapping from top to bottom is installed on the same axis, and they are arranged on separation column 601 1 sides.Condensation cooling water tank 619 is arranged on the downside of stripping tower 616,617,618, so that the condensation spiral coil cooling tube 620 that each oily stream can rely on potential difference to flow through automatically separately flows to subsequent processing.Water cooling tower 621 is installed in water tank 619 tops, and water circulating pump 622 is installed in water tank 619 bottoms one side, and hot water is pumped into water cooling tower 621, and following spray cooling recycles.
As Fig. 1, shown in Figure 9, gas-oil separation-gas absorbing device 7 of the present invention comprises gas-oil separation tower 701, one-level absorption column of gas 702, and secondary gas absorption tower 703, and water-sealed tank 704 etc., loading efficient Pall ring filler 705 in the two-level absorption tower 703.The I and II absorption tower will be blended in the objectionable constituent in the reaction cracked gas, remove as hydrogenchloride, hydrogen sulfide etc., send into liquefied gas retrieving arrangement 8.
As Fig. 1, shown in Figure 10, liquefied gas of the present invention (LPG) retrieving arrangement 8 comprises low-pressure gas stable can 801, introduce jar 801 from installing the 7 clean reacted gases of bringing, send into a stage compressor 802 behind the steady pressure, be compressed into 0.3～0.4Mpa, send into one-level compression fractional condensation flow container 803, in its jar condensation spiral coil cooling tube 804 is housed, the heavier liquefied gas components condense of part is become petroleum naphtha to be reclaimed, send into two stage compressor 805 again and be compressed to 0.5～0.8Mpa and take off reacted gas after the heavy constituent, send into condensate cooler 806 again, the liquefied gas component will be condensed into liquid this moment, be LPG, send into high-pressure liquid air separating tank 807 again, in these 807 jars, LPG and the dry gas (methane that can't compress and liquefy, ethane, ethylene component) separates, LPG goes into high-pressure liquefaction gas storage tank 808 from the jar underflow, and again through bottled pump 809, wiring 810 bottlings in some bottled minute are sold civilian.Dry gas is overflowed from 807 tank tops and is sent into high pressure dry gas stable can 811, and sends to stove behind the water seal back-fire relief jar 812 as personal fuel, if the unnecessary torch emptying or send boiler 12 (as the words that are provided with) to make fuel of setting fire is arranged.On the torch drop-out line of back-fire relief jar 812 self-forced type pressure automatic valve 813 is installed, it is controlling the full device system pressure.
As Fig. 1, shown in Figure 11, oil product extracting and refining device 9 of the present invention comprises gasoline-solar oil extracting system.They are by A-extractor 901,902, B-extractor 903,904, and additive tempering tank 905,906 etc. is formed.Gas oil, the raw gasline produced from scission reaction still and separation column still can not satisfy the GB specification of quality fully, need through refining.Gas oil is at first sent into A-extractor 801, add the A agent, carry out A-extracting and refining process, send into B-extractor 803 after removing undesirable components, add the B-extraction agent, send into tempering tank 805 again after further removing imperfect composition, add necessary additive according to performance requriements and be mixed into the sale of qualified product carrying device; Raw gasline extracting and refining process is also identical.
As Fig. 1, shown in Figure 12, " three wastes " of the present invention treatment unit 10 comprises that flue gas takes off black gas wash tower 1001, oil trap 1009 and efficient water-and-oil separator 1008.Gas wash tower 1001 is outside equipped with a water circulating pump 1004, is provided with a recirculation water shower nozzle 1005 in the gas wash tower 1001, and the stage casing is provided with a dividing plate 1006, and the lower-most point of dividing plate 1006 is provided with a fluid flow tube 1007.Efficient water-and-oil separator 1008 is arranged on after the oil trap 1009, is provided with a lift pump 1010 between the two.Lift pump 1010 is with oil trap 1009 isolated water, and pump is given efficient water-and-oil separator 1008, and the water purification after the purifying treatment returns by water circulating pump 1004 and supplies with gas wash tower 1001 uses.And oil trap 1009 and efficient water-and-oil separator 1008 isolated recovery of oil return reactor 301, continue cracking.
When the present invention uses, plastic waste is after removing silt particle, masonry, cotton, wood, iron filings etc., as shown in Figure 1 and Figure 2, send into the chapelet 101 that is arranged on forefront through preliminary fragmentation earlier, track type chain making machine 103 and the roll stacks 104 hot pressing rolls that surround via fume waste heat chuck stove 102 become plastic strip again, and, make plastic waste by the not enough 0.1t/m of tap density through cooling spray 110 and chopper 109
3Become 0.5～1.2t/m by density
3The plastics fritter.Can also send into crusher 11 (as shown in Figure 1) again, crusher 11 is arranged on after the hot pressing density roll device 1 but before elevated-temperature seal feeding device 2.The plastics stripping and slicing is crushed into 1 * 1cm
2Following fragment is sent into elevated-temperature seal feeding device 2 again.The plastic waste of elevated-temperature seal feeding unit 2 after with the density fragmentation adds reactor 301 hermetically continuously safely in reaction process, carry out catalytic cracking reaction, generates light fuel and gasoline, diesel oil distillate etc.When apparatus of the present invention are handled waste oil or mink cell focus simultaneously, being used for the tubular oven 12 of preheating waste oil and mink cell focus is set at before the reactor 301, and then make plastic waste and waste oil both can enter reactor 301 separately respectively, also can mix entering reactor 301 simultaneously by arbitrary proportion, be cracked into various light fuels or gasoline, diesel cut.The gas-oil mixture that is generated by reactor 301 is vapour phase and comes out to be introduced into separation column 601 from the top (as Fig. 1, shown in Figure 8, through separation column 601 fractionation, separation column 601 cats head go out gasoline and gas, the tower side line is extracted kerosene, light, heavy gas oil out, after weight diesel oil was liquid phase and flows into kerosene, light, heavy gas oil stripping tower 616,617,618 strippings, kerosene and solar oil unification and the heavy gas oil condensation cooling water tank 619 of flowing through cooled off.Separation column 601 cat head gasoline vapors and coal mine gas flow into gas-oil separation tower 701 (as Fig. 1, shown in Figure 9) after 619 coolings of condensation cooling water tank, gasoline passes back into separation column 601, thus control tower top temperature control quality of gasoline.The raw gasline of telling advances extracting and refining device 9; Coal mine gas is introduced liquefied gas retrieving arrangement 8 (as Fig. 1, shown in Figure 10) behind absorption cleanings such as absorption column of gas 702,703, tell civil liquefied gas and dry gas after liquefied gas retrieving arrangement 8 is handled, and this part dry gas can be used as personal fuel gas.Gasoline and solar oil are behind oil product extracting and refining device 901,902,903,904 extracting and refinings (as Fig. 1, shown in Figure 11), and suitably concocting through additive tempering tank 905,906 becomes processed oil again, and the oil product finished product goes out device thus.As Fig. 1, shown in Figure 12, flue gas takes off black gas wash tower 1001 and is arranged on after the reactor 301, be connected with the flue outlet 409 at ring set process furnace 404 tops, it can make the flue gas of discharge reduce to minimum to the pollution of environment black dirt particulate and the oxious component Ex-all in the flue gas.Efficient water-and-oil separator 1008 is arranged on after the oil product extracting and refining device 9, and it can be with waste oil waste water separating treatment, and waste oil returns reactor 301 cracking and reclaims, and sends into flue gas after wastewater treatment is clean and takes off black gas wash tower 1001 uses.
The present invention can all or part ofly as required select each device in the system of the present invention for use, and can increase some devices for system of the present invention, such as a waste gas cinder boiler 13 is set, be fuel with the cinder and the unnecessary gas of apparatus of the present invention output, produce steam etc.
Claims (10)
- But 1, a kind of plastic waste oilization device of continuous industry production, it comprises: reactor, the feeding unit that connects described reactor, heating unit for described reactor reaction, be arranged on the coke discharging device of described reactor bottom, be connected to described reactor fractionation-stripping-condensation refrigerating unit afterwards in turn, gas-oil separation-gas absorbing device, oil product extracting and refining device, and the liquefied gas retrieving arrangement of drawing by gas-oil separation-gas absorbing device; It is characterized in that:It also comprises by having flue gas takes off the three wastes processing unit of black dedusting and waste oil waste water treatment and reclamation function, described flue gas takes off the flue outlet that black cleaning apparatus connects described heating unit, the waste oil waste water treatment and reclamation device of described " three wastes " treatment unit connects described oil product extracting and refining device, described waste oil waste water treatment and reclamation device comprises oil trap and water-and-oil separator, the water side of described oil trap connects described water-and-oil separator by lift pump, the water side of described water-and-oil separator connects described recirculation water shower nozzle by the outer water circulating pump of described gas wash tower, the oil outlet end of described oil trap and water-and-oil separator is connected back described reactor, continues cracking; The flue gas of described " three wastes " treatment unit takes off black gas wash tower and is divided into two sections, epimere is spray quinoline gas wash tower, hypomere is the water seal dedusting absorption tower, described gas wash tower is outside equipped with water circulating pump, be provided with the recirculation water shower nozzle in the described gas wash tower, described gas wash tower stage casing is provided with dividing plate, and described dividing plate lower-most point is provided with fluid flow tube; Described feeding unit comprises hot pressing density roll device and elevated-temperature seal feeding device two portions, described hot pressing density roll device comprises chapelet, the flue gas chuck stove that is connected with chapelet, be arranged on track type chain making machine and hot pressing density roll stacks in the described chuck stove, be arranged on the conveying belt below the described hot pressing density roll stacks, be arranged on the water-cooling-sprayer of described conveying belt top and gantry chopper that described conveying belt exports is set, be arranged on the cooling basin of described chopper below and the scraper-type chain making machine that sets within it to described elevated-temperature seal feeding device convey materials.Described heating unit is non-naked light radiation formula heating unit, and described coke discharging device is made up of the coke discharging guiding valve of 2～3 coke discharging jars and 3 interlockings.
- But 2, the plastic waste oilization device of continuous industry production as claimed in claim 1, it is characterized in that: it comprises that also one is arranged on the plastic breaker between described hot pressing density roll device and the elevated-temperature seal feeding device, and one is arranged on before the described reactor and carries the tubular oven of hot waste oil and mink cell focus to described reactor.
- 3, but the plastic waste oilization device of continuous industry production as claimed in claim 1, it is characterized in that: described elevated-temperature seal feeding device comprises by frequency control motor drive lift, be connected described lift and the band stirrer loading hopper between the blanking inclined tube, the reinforced forcing machine of molten formula is moulded in the sealing that connects described loading hopper, described forcing machine comprises the pushing screw rod that is driven by frequency control motor and is looped around described pushing screw rod barrel on every side, be provided with heating flue gas chuck in the exit of described forcing machine, vertical connection one casing drum in the exit of described forcing machine, the top of described casing drum is provided with one and discloses the material mechanical manipulator, and the bottom of described casing drum is connected described reactor by the thermal expansion joint with the valve that feeds in raw material.
- 4, but the plastic waste oilization device of continuous industry production as claimed in claim 2, it is characterized in that: described elevated-temperature seal feeding device comprises by frequency control motor drive lift, be connected described lift and the band stirrer loading hopper between the blanking inclined tube, the reinforced forcing machine of molten formula is moulded in the sealing that connects described loading hopper, described forcing machine comprises the pushing screw rod that is driven by frequency control motor and is looped around described pushing screw rod barrel on every side, be provided with heating flue gas chuck in the exit of described forcing machine, vertical connection one casing drum in the exit of described forcing machine, the top of described casing drum is provided with one and discloses the material mechanical manipulator, and the bottom of described casing drum is connected described reactor by the thermal expansion joint with the valve that feeds in raw material.
- 5, but plastic waste oilization device as claim 1 or 2 or 3 or 4 described continuous industry productions, it is characterized in that: described non-naked light radiation formula heating unit comprises the roasting kiln that is arranged on the marmon clamp blind roaster around the described reactor and is arranged on described reactor bottom, one annular is led flame cover or six and is led flame tube and be communicated with described marmon clamp blind roaster and roasting kiln, on described roasting kiln, be provided with one deck resistance flame plate, and described resistance flame plate is provided with the resistance flame aperture that is evenly distributed, both sides at described roasting kiln are provided with a burner respectively, the crater of described burner tilts along the furnace wall direction, the flame of ejection is formed in burner hearth revolve flame.
- But 6, as the plastic waste oilization device of claim 1 or 2 or 3 or 4 described continuous industry productions, it is characterized in that: described high temperature interlocking coke discharging device comprises one-level coke discharging jar and the secondary coke discharging jar that the first coke discharging guiding valve on the coke discharging tube is connected bottom described reactor, be connected second guiding valve between the described I and II coke discharging jar and be connected the 3rd guiding valve below the secondary coke discharging jar, described three guiding valve interlocking coke dischargings, described one-level coke discharging jar are provided with two coke discharging mechanical manipulators and and visit burnt mechanical manipulator.
- But 7, the plastic waste oilization device of continuous industry production as claimed in claim 5, it is characterized in that: described high temperature interlocking coke discharging device comprises one-level coke discharging jar and the secondary coke discharging jar that the first coke discharging guiding valve on the coke discharging tube is connected bottom described reactor, be connected second guiding valve between the described I and II coke discharging jar and be connected the 3rd guiding valve below the secondary coke discharging jar, described three guiding valve interlocking coke dischargings, described one-level coke discharging jar are provided with two coke discharging mechanical manipulators and and visit burnt mechanical manipulator.
- 8, but plastic waste oilization device as claim 1 or 2 or 3 or 4 or 7 described continuous industry productions, it is characterized in that: described high temperature interlocking coke discharging device comprises the coke discharging jar of the conversion operation of three parallel connections, wherein a positive coke discharging jar be arranged on the same axis of the coke discharging tube of described reactor on, in addition the central axis of two described coke discharging jars and described positive coke discharging jar is an angle and is arranged on a left side, right both sides, and the downward-sloping first-class burnt gradient of two coke discharging jars difference about described, described three coke discharging jars connect the coke discharging tube of described reactor respectively by a coke discharging guiding valve, and described three guiding valve interlocking coke dischargings, described each coke discharging jar is provided with a coke discharging mechanical manipulator.
- 9, but the plastic waste oilization device of continuous industry production as claimed in claim 5, it is characterized in that: described high temperature interlocking coke discharging device comprises the coke discharging jar of the conversion operation of three parallel connections, wherein a positive coke discharging jar be arranged on the same axis of the coke discharging tube of described reactor on, in addition the central axis of two described coke discharging jars and described positive coke discharging jar is an angle and is arranged on a left side, right both sides, and the downward-sloping first-class burnt gradient of two coke discharging jars difference about described, described three coke discharging jars connect the coke discharging tube of described reactor respectively by a coke discharging guiding valve, and described three guiding valve interlocking coke dischargings, described each coke discharging jar is provided with a coke discharging mechanical manipulator.
- 10, but the plastic waste oilization device of continuous industry production as claimed in claim 6, it is characterized in that: described high temperature interlocking coke discharging device comprises the coke discharging jar of the conversion operation of three parallel connections, wherein a positive coke discharging jar be arranged on the same axis of the coke discharging tube of described reactor on, in addition the central axis of two described coke discharging jars and described positive coke discharging jar is an angle and is arranged on a left side, right both sides, and the downward-sloping first-class burnt gradient of two coke discharging jars difference about described, described three coke discharging jars connect the coke discharging tube of described reactor respectively by a coke discharging guiding valve, and described three guiding valve interlocking coke dischargings, described each coke discharging jar is provided with a coke discharging mechanical manipulator.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100580183A CN1250677C (en) | 2004-08-06 | 2004-08-06 | Waste plastic oiling device for continuous industrial production at large scale |
| PCT/CN2005/001195 WO2006012800A1 (en) | 2004-08-06 | 2005-08-04 | An apparatus for preparing oil from waste plastics in continuous and industrial production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100580183A CN1250677C (en) | 2004-08-06 | 2004-08-06 | Waste plastic oiling device for continuous industrial production at large scale |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1587350A CN1587350A (en) | 2005-03-02 |
| CN1250677C true CN1250677C (en) | 2006-04-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100580183A Expired - Fee Related CN1250677C (en) | 2004-08-06 | 2004-08-06 | Waste plastic oiling device for continuous industrial production at large scale |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN1250677C (en) |
| WO (1) | WO2006012800A1 (en) |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008022790A2 (en) * | 2006-08-25 | 2008-02-28 | Granit Systems S.A. | Method and device for processing plastic-containing waste |
| CN101851523B (en) * | 2010-06-01 | 2013-02-20 | 上海劲飚环保科技有限公司 | Continuous waste plastics refining unit |
| CN102210960B (en) * | 2011-06-10 | 2013-06-05 | 济南世纪华泰科技有限公司 | Technology and equipment for dedusting mixed oil gas |
| CN102925169B (en) * | 2012-11-13 | 2014-05-21 | 中冶焦耐工程技术有限公司 | Coke discharging process of semi-coke |
| CN103521157A (en) * | 2013-10-25 | 2014-01-22 | 滁州市全丰物资有限公司 | Large-size reaction equipment for synthesizing polyester resin |
| CN104930513A (en) * | 2015-07-02 | 2015-09-23 | 周海波 | Fuel-gas-catalyzing flameless near-infrared direct heating porous medium combustor |
| CN108217777A (en) * | 2018-02-12 | 2018-06-29 | 四川旭航新材料有限公司 | A kind of water-oil separating module, oil-water separation system and method |
| CN108913165A (en) * | 2018-09-20 | 2018-11-30 | 陕西冶金设计研究院有限公司 | A kind of oil shale retorting semicoke dry method goes out coke installation |
| CN111377589B (en) * | 2018-12-31 | 2022-05-06 | 潍坊奥华环保新材料科技有限公司 | Automatic gas injection charging process for producing rock wool electric melting furnace |
| CN111205884B (en) * | 2020-03-11 | 2022-02-15 | 张忠余 | Waste plastic oil refining equipment |
| CN111500305B (en) * | 2020-04-28 | 2024-02-20 | 徐宗胜 | Waste plastic treatment equipment |
| CN114164022B (en) * | 2021-11-24 | 2023-06-09 | 成都前成科技有限公司 | Etherification and solvent refining process for plastic reclaimed oil |
| CN115155100A (en) * | 2022-06-02 | 2022-10-11 | 贵阳晨光生物科技有限公司 | Automatic supercritical extraction method |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR0140957B1 (en) * | 1993-07-29 | 1998-06-15 | 후지이 요시히로 | Apparatus for thermally decomposing plastics and process for converting plastics into oil by thermal decomposition |
| JP3276546B2 (en) * | 1995-10-23 | 2002-04-22 | 三菱重工業株式会社 | Method of converting chlorine-containing plastic waste to oil |
| CN1127554C (en) * | 2000-07-12 | 2003-11-12 | 北京乐意环保技术有限公司 | Technological process and equipment of utilizing waste plastics to product gasoline, desel oil and liquiefied gas |
| CN2513996Y (en) * | 2001-12-04 | 2002-10-02 | 姜皓 | Waste plastic oil refining device capable of continuously industrialized production |
-
2004
- 2004-08-06 CN CNB2004100580183A patent/CN1250677C/en not_active Expired - Fee Related
-
2005
- 2005-08-04 WO PCT/CN2005/001195 patent/WO2006012800A1/en active Application Filing
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| Publication number | Publication date |
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| CN1587350A (en) | 2005-03-02 |
| WO2006012800A1 (en) | 2006-02-09 |
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